Dual catalyst system for propylene production

ABSTRACT

Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm3/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst.

CROSS REFERENCE TO RELATED APPLICATION

This application is filed as a continuation of U.S. application Ser. No.15/190,981 filed on Jun. 23, 2016 which claims the benefit of U.S.Provisional Application Ser. No. 62/188,178 filed Jul. 2, 2015.

TECHNICAL FIELD

Embodiments of the present disclosure generally relate to propyleneproduction via metathesis reactions, and more specifically relate toconverting butene to propylene using a dual catalyst system comprisingmetathesis and cracking catalysts.

BACKGROUND

In recent years, there has been a dramatic increase in the demand forpropylene to feed the growing markets for polypropylene, propylene oxideand acrylic acid. Currently, most of the propylene produced worldwide(74 million tons/year) is a by-product from steam cracking units (57%)which primarily produce ethylene, or a by-product from Fluid CatalyticCracking (FCC) units (30%) which primarily produce gasoline. Theseprocesses cannot respond adequately to a rapid increase in propylenedemand.

Other propylene production processes contributes about 12% of totalpropylene production. Among these processes are propane dehydrogenation(PDH), metathesis reactions requiring both ethylene and butene, highseverity FCC, olefins cracking and methanol to olefins (MTO). However,propylene demand has exceeded ethylene and gasoline/distillate demand,and propylene supply has not kept pace with this increase in propylenedemand.

SUMMARY

Accordingly, ongoing needs exist for improved processes for theselective production of propylene using dual catalyst systems.Embodiments of the present disclosure are directed to propyleneproduction from butenes via a dual catalyst system.

In one embodiment, a process for the production of propylene isprovided. The process comprises providing a dual catalyst systemcomprising: a mesoporous silica catalyst impregnated with metal oxide,and a mordenite framework inverted (MFI) structured silica catalystdownstream of the mesoporous silica catalyst. The mesoporous silicacatalyst includes a total pore volume of at least about 0.600 cm³/g, andthe MFI structured silica catalyst includes a total acidity of 0.001mmol/g to 0.1 mmol/g. The process also comprises producing propylenefrom a stream comprising butene via metathesis and cracking bycontacting the stream comprising butene with the dual catalyst system,where the stream comprising butene contacts the mesoporous silicacatalyst before contacting the MFI structured silica catalyst.

In another embodiment, a dual catalyst system for producing propylenefrom butene is provided. The dual catalyst system comprises a metathesiscatalyst zone and a cracking catalyst zone downstream of the metathesiscatalyst zone. The metathesis catalyst zone comprises mesoporous silicacatalyst impregnated with metal oxide, where the mesoporous silicacatalyst includes a pore size distribution of at least 2.5 nm to 40 nmand a total pore volume of at least 0.600 cm³/g. The cracking catalystzone comprises a mordenite framework inverted (MFI) structured silicacatalyst, where the MFI structured silica catalyst includes a pore sizedistribution of at least 1.5 nm to 3 nm, and a total acidity of 0.001mmol/g to 0.1 mmol/g.

Additional features and advantages of the described embodiments will beset forth in the detailed description which follows, and in part will bereadily apparent to those skilled in the art from that description orrecognized by practicing the described embodiments, including thedetailed description which follows, the claims, as well as the appendeddrawings.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is an X-ray Powder Diffraction (XRD) graph illustrating the XRDprofile of a CARiACT Q10 support, and a CARiACT Q10 support impregnatedwith WO₃ at a molar ratio of silica/WO₃ equal to approximately 10 inaccordance with one or more embodiments of the present disclosure.

FIG. 2 is an XRD graph of a MFI-2000 catalyst.

FIG. 3 is a Scanning Electron Microscopy (SEM) image of a CARiACT Q10support.

FIG. 4 is an SEM image of a CARiACT Q10 support impregnated with 10% byweight WO₃ in accordance with one or more embodiments of the presentdisclosure.

FIG. 5 is an SEM image of a of MFI-2000 catalyst.

DETAILED DESCRIPTION

Embodiments of the present disclosure are directed to systems andmethods for converting a stream comprising butene to a stream comprisingpropylene via catalyzed metathesis and catalyzed cracking. Specifically,the present embodiments are related to a two-stage catalyst systemcontaining metathesis and cracking catalysts for greater propylene (C₃═)production from a butene stream. In operation, the metathesis catalystis followed by the cracking catalyst to provide a greater yield ofpropylene, and optionally a greater combined yield of propylene andethylene.

As shown in the following Formulas 1 and 2, “metathesis” or“self-metathesis” is generally a two-step process: 2-buteneisomerization and then cross-metathesis using the metathesis catalystsystem. As shown in the following Formula 3, “catalyzed cracking” refersto the conversion of C₄-C₆ alkenes to propylene and other alkanes and/oralkenes, for example, C₁-C₂ alkenes.

Referring to Formulas 1-3, the “metathesis” and “catalytic cracking”reactions are not limited to these reactants and products; however,Formulas 1-3 provide a basic illustration of the reaction methodology.As shown in Formulas 1 and 2, metathesis reactions take place betweentwo alkenes. The groups bonded to the carbon atoms of the double bondare exchanged between the molecules to produce two new alkenes with theswapped groups. The specific catalyst that is selected for the olefinmetathesis reaction may generally determine whether a cis-isomer ortrans-isomer is formed, as the coordination of the olefin molecules withthe catalyst play an important role, as do the steric influences of thesubstituents on the double bond of the newly formed molecule.

The present dual catalyst system comprises: a mesoporous silicacatalyst, which is a mesoporous silica catalyst support impregnated withmetal oxide; and a mordenite framework inverted (MFI) structured silicacatalyst downstream of the mesoporous silica catalyst. Variousstructures are contemplated for the mesoporous silica catalyst support,for example, a molecular sieve. As used in the application, “mesoporous”means that the silica support has a narrow pore size distribution.Specifically, the mesoporous silica catalyst includes a narrow pore sizedistribution of from about 2.5 nm to about 40 nm and a total pore volumeof at least about 0.600 cm³/g. Without being bound by theory, thepresent pore size distribution and pore volume are sized to achievebetter catalytic activity and reduced blocking of pores by metal oxides,whereas smaller pore volume and pore size catalyst systems aresusceptible to pore blocking and thereby reduced catalytic activity.

Moreover, utilizing an MFI structured silica catalyst downstream of themesoporous silica catalyst surprisingly provides the best yield ofpropylene from a butene stream. The person of ordinary skill in the artwould have expected the best yield by first cracking butene to propyleneand then cracking any remaining butene via metathesis. However, it wassurprisingly found that propylene yield is increased, and additionallythe combined yield of propylene and ethylene is increased by placing theMFI structured silica catalyst downstream of the mesoporous silicacatalyst.

In one or more embodiments, the pore size distribution of the mesoporoussilica catalyst may range from about 2.5 nm to about 40 nm, or about 2.5nm to about 20 nm, or about 2.5 nm to about 4.5 nm, or about 2.5 nm toabout 3.5 nm, or about 8 nm to about 18 nm, or about 12 nm to about 18nm. In further embodiments, the total pore volume may be from about0.600 cm³/g to about 2.5 cm³/g, or about 0.600 cm³/g to about 1.5 cm³/g,or about 0.600 cm³/g to about 1.3 cm³/g, or about 0.600 cm³/g to about0.800 cm³/g, or about 0.600 cm³/g to about 0.700 cm³/g, or about 0.900cm³/g to about 1.3 cm³/g.

Moreover, while broader ranges are contemplated, the mesoporous silicacatalyst may, in one or more embodiments, include a surface area ofabout 250 meters/gram (m²/g) to about 600 m²/g. In further embodiments,the mesoporous silica catalyst may have a surface area of from about 450m²/g to about 600 m²/g, or about 250 m²/g to about 350 m²/g, or about275 m²/g to about 325 m²/g, or about 275 m²/g to about 300 m²/g.Further, the mesoporous silica catalyst may have a total acidity of upto about 0.5 millimole/gram (mmol/g), or about 0.01 mmol/g to about 0.5mmol/g, or about 0.1 mmol/g to about 0.5 mmol/g, or about 0.3 mmol/g toabout 0.5 mmol/g, or about 0.4 mmol/g to about 0.5 mmol/g. Acidity isgenerally maintained at or less than about 0.5 mmol/g to yield thedesired selectivity of propylene and reduced production of undesirablebyproducts such as aromatics. Increasing acidity may increase theoverall butene conversion; however, this increased conversion may leadto less selectivity and increased production of aromatic byproducts,which can lead to catalyst coking and deactivation.

Furthermore, the mesoporous silica catalyst may have a particle size offrom about 20 nm to about 200 nm, or about 50 nm to about 150 nm, orabout 75 nm to about 125 nm. In additional embodiments, the mesoporoussilica catalyst may have an individual crystal size of about 1 μm toabout 100 μm, or about 10 μm to about 40 μm.

Various formulations for the mesoporous silica support, as well asmethods of making the formulation, are contemplated. For example, themesoporous silica catalyst support may be produced via wet impregnation,hydrothermal synthesis, or both. Additionally, the mesoporous silicacatalyst support may be characterized by an ordered pore structure. Forexample, this ordered structure may have a hexagonal array of pores. Onesuitable embodiment of a mesoporous silica support with a hexagonal porearray may be the Santa Barbara Amorphous (SBA-15) mesoporous silicamolecular sieve. Alternatively, another suitable embodiment of amesoporous silica support is the CARiACT Q-10 (Q-10) spherical catalystsupport produced by Fuji Silysia Chemical Ltd.

The catalyst of the metathesis reaction is the impregnated metal oxideof the silica support. The metal oxide may comprise one or oxides of ametal from the Groups 6-10 of the IUPAC Periodic Table. In one or moreembodiments, the metal oxide may be an oxide of molybdenum, rhenium,tungsten, or combinations thereof. In a specific embodiment, the metaloxide is tungsten oxide (WO₃). It is contemplated that various amountsof metal oxide may be impregnated into the mesoporous silica catalystsupport. For example and not by way of limitation, the molar ratio ofsilica to metal oxide, for example, WO₃, is about 5 to about 60, orabout 5 to about 15, or about 20 to about 50, or about 20 to about 40,or about 25 to about 35.

Additionally, various silica structures are contemplated for the MFIstructured silica catalyst. For example, the MFI structured silicacatalyst may include MFI structured aluminosilicate zeolite catalysts orMFI structured silica catalysts free of alumina. As used herein, “free”means less than 0.001% by weight of alumina in the MFI structured silicacatalyst. Moreover, it is contemplated that the MFI structured silicacatalyst may include other impregnated metal oxides in addition to or asan alternative to alumina. Like the mesoporous silica catalyst, the MFIstructured catalysts may have alumina, metal oxides, or both impregnatedin the silica support. In addition to or as a substitute for alumina, itis contemplated to include the metal oxides listed prior, specifically,one or more oxides of a metal from Groups 6-10 of the IUPAC PeriodicTable, more specifically, metal oxides of molybdenum, rhenium, tungsten,titanium, or combinations thereof.

For the MFI structured aluminosilicate zeolite catalysts, variousamounts of alumina are contemplated. In one or more embodiments, the MFIstructured aluminosilicate zeolite catalysts may have a molar ratio ofsilica to alumina of about 5 to about 5000, or about 100 to about 4000,or about 200 to about 3000, or about 1500 to about 2500, or about 1000to about 2000. Various suitable commercial embodiments of the MFIstructured aluminosilicate zeolite catalysts are contemplated, forexample, ZSM-5 zeolites such as MFI-280 produced by ZeolystInternational or MFI-2000 produced by Saudi Aramco.

Various suitable commercial embodiments are also contemplated for thealumina free MFI structured catalysts. One such example is Silicalite-1produced by Saudi Aramco.

The MFI structured silica catalyst may include a pore size distributionof from about 1.5 nm to 3 nm, or about 1.5 nm to 2.5 nm. Furthermore,the MFI structured silica catalyst may have a surface area of from about300 m²/g to about 425 m²/g, or about 340 m²/g to about 410 m²/g.Additionally, the MFI structured silica catalyst may have a totalacidity of from about 0.001 mmol/g to about 0.1 mmol/g, or about 0.01mmol/g to about 0.08 mmol/g. The acidity is maintained at or less thanabout 0.1 mmol/g in order to reduce production of undesirable byproductssuch as aromatics. Increasing acidity may increase the amount ofcracking; however, this increased cracking may also lead to lessselectivity and increased production of aromatic byproducts, which canlead to catalyst coking and deactivation.

In some cases, MFI structured silica catalyst may be modified with anacidity modifier to adjust the level of acidity in the MFI structuredsilica catalyst. For example, these acidity modifiers may include rareearth modifiers, phosphorus modifiers, potassium modifiers, orcombinations thereof. However, as the present embodiments are focused onreducing the acidity to a level at or below 0.1 mmol/g, the presentstructured silica catalyst may be free of acidity modifier, such asthose selected from rare earth modifiers, phosphorus modifiers,potassium modifiers, or combinations thereof. As used herein, “free ofacidity modifiers” means less than less than 0.001% by weight of aciditymodifier in the MFI structured silica catalyst.

Further, the MFI structured silica catalyst may have a pore volume offrom about 0.1 cm³/g to about 0.3 cm³/g, or about 0.15 cm³/g to about0.25 cm³/g. Additionally, the MFI structured silica catalyst may have anindividual crystal size ranging from about 10 nm to about 40 μm, or fromabout 15 μm to about 40 μm, or from about 20 μm to about 30 μm. Inanother embodiment, the MFI structured silica catalyst may have anindividual crystal size in a range of from about 1 μm to about 5 μm.

Moreover, various amounts of each catalyst are contemplated for thepresent dual catalyst system. For example, it is contemplated that theratio by volume of metathesis catalyst to cracking catalyst may rangefrom about 5:1 to about 1:5, or about 2:1 to about 1:2, or about 1:1.

In operation, a product stream comprising propylene is produced from abutene containing stream via metathesis conversion by contacting thebutene stream with the dual catalyst system. The butene stream maycomprise 2-butene, and optionally comprises one or more isomers, such as1-butene, trans-2-butene, and cis-2-butene. The present discussioncenters on butene based feed streams; however, it is known that otherC₁-C₆ components may also be present in the feed stream.

The mesoporous silica catalyst is a metathesis catalyst whichfacilitates isomerization of 2-butene to 1-butene followed bycross-metathesis of the 2-butene and 1-butene into a metathesis productstream comprising propylene, and other alkenes/alkanes such as pentene.The MFI structured silica catalyst, which is downstream of themetathesis catalyst, is a cracking catalyst which produces propylenefrom C₄ or C₅ olefins in the metathesis product stream, and may alsoyield ethylene.

It is contemplated that the metathesis catalyst and the crackingcatalyst are disposed in one reactor or multiple reactors. For example,it may be desirable to use separate reactors for the metathesis andcracking catalysts when they operate at different environmentalconditions, including temperature and pressure. Regardless of whetherone or multiple reactors contain the dual catalysts, the dual catalystsystem will have a metathesis catalyst zone or section and a downstreamcracking catalyst zone or section. For example, the mesoporous silicametathesis catalyst may be located in the top part of the reactor andthe MFI structured silica cracking catalyst may be disposed in thebottom part of the reactor, assuming the reactant stream enters the topportion of the reactor. For example, each catalyst may be positioned asdiscrete catalyst beds. Moreover, it is contemplated that the twocatalysts of the dual catalyst system may be in contact with one anotheror separated. However, if the metathesis catalyst and cracking catalystare in contact, it is desirable that the metathesis catalyst is stilldisposed upstream of the cracking catalyst. The catalysts can be used inthe same reactor or with different reactors arranged in series.Alternatively, it is contemplated that the metathesis catalyst(mesoporous silica catalyst) is disposed in a first reactor and thecracking catalyst (MFI structured silica catalyst) is disposed in aseparate second reactor downstream of the first reactor. In specificembodiments, there is a direct conduit between the first reactor andsecond reactor, so that the cracking catalyst can directly crack theproduct of the butene metathesis reaction. Various systems whichincorporate the catalyst system are contemplated. For details regardingsuch systems, Saudi Aramco U.S. Application No. 62/188,052 entitledSystems and Methods of Producing Propylene is incorporated by referencein its entirety.

Various methods of making the catalysts used in the dual catalyst systemare contemplated. Specifically, the processes of wet impregnation andhydrothermal synthesis may be utilized; however, other catalystsynthesis techniques are also contemplated.

Various operating conditions are contemplated for the contacting of thebutene stream with the dual catalyst system. For example, the butenestream may contact the dual catalyst system at a space hour velocity ofabout 10 to about 10,000 h⁻¹, or about 300 to about 1200 h⁻¹. Moreover,the butene stream may contact the catalyst system at a temperature offrom about 200 to about 600° C., or about 300 to about 600° C.Furthermore, the butene stream may contact the catalyst system at apressure from about 1 to about 30 bars, or about 1 to about 10 bars.

Optionally, the dual catalyst system may be pretreated prior tometathesis and/or cracking. For example, the dual catalyst system may bepretreated with N₂ for about 1 hour to about 5 hours before metathesisat a temperature of at least about 400° C., or at least about 500° C.

The product stream yielded by the dual catalyst system may have at leastan 80 mol. % conversion of butene and a propylene yield in mol. % of atleast 40%. In a further embodiment, the product stream may have at leastan 85 mol. % conversion of butene and a propylene yield in mol. % of theat least 45%. Moreover, the product stream may have at least a 15 mol. %yield of ethylene, or at least a 20 mol. % yield of ethylene. In yetanother embodiment, the product stream may have at least 45 mol. % yieldof propylene, or at least about a 50 mol. % yield of propylene.

Moreover, the product stream may comprise less than 1 about wt %aromatics, or less than about 5 wt % of alkanes and aromatics. Withoutbeing bound by theory, in some embodiments it may be desirable that thearomatics and alkanes yield be low as it indicates coke formation, whichmay result in catalyst deactivation.

EXAMPLES

The following examples show the preparation of various catalysts whichare used in a combination as in the present dual catalysts.

Example 1: Preparation of W-SBA-15(30)

Sodium tungstate was used as the source of tungsten ion for thesynthesis of W-SBA-15 by direct hydrothermal method. In a typicalsynthesis of W-SBA-15, tungsten was incorporated into the framework ofmesoporous support SBA-15 depending upon the Si/W molar ratio. Pluronic®123 (P123) was dissolved in HCl and tetraethylorthosilicate (TEOS) wasadded with vigorous stirring. Then, a calculated amount of sodiumtungstate solution was added to the solution and stirred at 95° C. for 3days under hydrothermal conditions. The resultant solid was filtered,dried and calcined at 550° C. for 5 hours. The catalysts obtained inthis way were identified as W-SBA-15(30), where 30 represents the molarratio of silicon to tungsten (Si/W). The molar ratio of the gelcomposition is 1 SiO₂:0.3-0.6 WO₃:0.0167 P123:5.82 HCl:190H₂O.

Example 2: Preparation of Silicalite-1

In a typical synthesis, 4.26 grams (g) tetrapropylammonium bromide (TPA)and 0.7407 g ammonium fluoride was dissolved in 72 ml of water andstirred well for 15 minutes. Then, 12 g fumed silica was added andstirred well until homogenized. The obtained gel was autoclaved and keptat 200° C. for 2 days. The molar composition of gel was 1 SiO₂: 0.08(TPA)Br: 0.10 NH₄F: 20H₂O. The solid products obtained were washed withwater and dried at 80° C. overnight. The template was removed bycalcination in air at 750° C. for 5 hours.

Example 3: Preparation of MFI-2000

In a typical synthesis, 4.26 g TPA and 0.7407 g ammonium fluoride wasdissolved in 72 ml of water and stirred well for 15 minutes. 12 g fumedsilica was added and stirred well until homogenized. An appropriateamount of aluminum sulfate was added and the obtained gel was autoclavedand kept at 200° C. for 2 days. The molar composition of gel was 1 SiO₂:0.0005 Al₂O₃: 0.08 (TPA)Br: 0.10 NH₄F: 20H₂O. The solid productsobtained were washed with water and dried at 80° C. overnight. Thetemplate was removed by calcination in air at 550° C. for 5 hours.

Example 4: Preparation of 10WO₃/Q10

10WO₃/CARiACT Q10 was prepared by the wet impregnation method. Anaqueous solution of ammonium metatungstate [(NH₄)6H₂W₁₂O₄₀.xH₂O] and thecommercial silica support were mixed together and dried in an oven at110° C. for 12 hours and calcined at 550° C. for 8 hours. As shown inTable 1 as follows, the supported tungsten oxide catalyst (10WO₃/Q10)has a lower surface area when compared to the parent Q10 material,indicating the presence of tungsten oxide on the support.

The SEM images of CARiACT Q10 support and 10WO₃/Q10 catalyst are shownin FIGS. 1 and 2, respectively. Both the CARiACT Q10 support and thetungsten loaded 10WO₃/Q10 have a particle size in the range of 75-125nm. Lack of agglomeration of tungsten oxide particles in 10WO₃/Q10indicates a high dispersion of tungsten oxide on the support. Referringto FIG. 2, the SEM image of MFI-2000 shows a uniform particle sizedistribution with crystal size of about 35-50 μm. The X, Y, and Z axisof crystal are 50 μm, 16 μm, and 3 μm, respectively.

The XRD patterns of Q10, 10WO₃/Q10 and the MFI-2000 materials are shownin FIGS. 3-5. Referring to FIG. 4, the Q10 support shows a broad peak at15-20° indicating the presence of amorphous silica in the material.Further referring to FIG. 4, the 10WO₃/Q10 catalyst shows peaks at23.09, 23.57, 24.33 and 34.01 corresponding to the crystalline phase ofWO₃. This shows the presence of WO₃ species in the catalyst. As shown inFIG. 5, the XRD patterns of MFI-2000 exhibit peaks characteristic of theMFI structure in the ranges 8-9° and 22-25°. The intensity of the peakat 20=8.8° is comparable with the peaks in the range 22-25° indicatingthe formation of zeolite crystals along the b-axis.

Example 5: Catalyst Properties

Table 1 includes mechanical properties of the catalysts prepared inExamples 1-4, plus MFI 280 which is prepared similarly to MFI-2000 asdisclosed in Example 3.

TABLE 1 BET Surface Pore Pore Size Total Area Volume Distributionacidity Catalysts/Supports (m²/g) (cm³/g) (nm) (mmol/g) MetathesisCatalysts/Supports W-SBA-15 501 0.78 6.9 0.46 (Si/W = 30) CARiACT Q10300 1.00 100 10WO₃/Q10 279 1.22 17.5 0.09 Cracking Catalysts MFI-280 4000.23 2.0 0.07 MFI-2000 367 0.19 2.0 0.01 Silicalite-1 348 0.23 2.0 Notdetected

Example 6: Catalyst Performance of W-SBA-15 with Cracking Catalysts

The prepared catalysts from Examples 1-4 were tested for their activityand selectivity to butene metathesis reaction in a fixed bed continuousflow reactor (ID 0.25 in, Autoclave Engineers Ltd.) at atmosphericpressure. A fixed amount of catalyst samples, 1 ml of each catalyst type(with a total of 2 ml) was packed in the reactor tube with siliconcarbide on top and bottom of the reactor. The catalysts were pretreatedunder N₂ at 550° C. for 1 hour. All reactions were carried out at atemperature of 550° C., a GHSV (gas hourly space velocity) of 900 h⁻¹,and atmospheric pressure using 2-butene (5 milliliters/minutes (ml/min))as feed with nitrogen as diluent (25 ml/min). The quantitative analysisof the reaction products were carried out on-line using Varian gaschromatograph with flame ionization detector (FID) (Varian 450-GC),equipped with GasPro porous layer open tubular column.

Table 2 indicates the catalytic performances of cracking catalystsMFI-280 and MFI-2000 individually and in a combination (dual) mode withcatalyst W-SBA-15(30) in the metathesis and cracking reaction of2-butene (Reaction temperature: 550° C., atmospheric pressure, GHSV of900 h⁻¹). It can be seen that the combination of W-SBA-15 metathesiscatalyst with downstream MFI-2000 cracking catalyst offered the highestyields of propylene.

TABLE 2 Product W-SBA-15(30) W-SBA-15(30) Component MFI-280 MFI-280MFI-2000 MFI-2000 Conversion 95.67 94.16 93.72 91.00 2-C₄ (%) C₂═ 30.5329.61 30.29 22.99 C₃═ 29.14 33.19 38.98 45.46 1-C₄═ 1.82 2.50 2.91 4.21Isobutylene 3.92 5.72 5.96 8.52 C₅═ 1.81 2.88 2.31 3.98 C₆═ 0.00 0.000.00 0.32

Table 3 shows the catalytic performance of individual catalystW-SBA-15(30) and a dual W-SBA-15(30)/silicalite-1 catalyst in themetathesis and cracking reaction of 2-butene (Reaction temperature: 550°C., atmospheric pressure, GHSV of 900 hr⁻¹).

TABLE 3 W-SBA-15(30) & Product Component W-SBA-15(30) Silicalite-1Conversion 2-C₄ (%) 81.69 87.03 C₂═ 11.48 14.87 C₃═ 35.54 43.58 1-C₄═8.06 5.80 Isobutylene 3.24 11.28 C₅═ 15.05 8.09 C₆═ 4.20 0.38

Example 7: Catalyst Performance of CARiACT Q10 with Cracking Catalysts

The catalyst performance was also evaluated for the CARiACT Q10metathesis catalyst as described in Example 4. The catalytic reaction of2-butene (1:1 mixture of trans-2-butene & cis-2-butene) was performed ina fixed-bed tubular reactor (grade 316 stainless steel tube with an IDof 0.312 inches, OD of 0.562 inches and a length of 8 inches). In theexperiment, the reactor is charged with 2 ml of the catalyst(single-bed) previously sieved to a particle size of 0.5-1.0 mmdiameter. The catalyst sample was first activated in a nitrogen streamat 550° C. for 1 hours. The flow rates of feed (2-Butene) and N₂ weremaintained at 5.0 ml/min and 25 ml/min, respectively, during thereaction. The reaction was carried out at a temperature of 550° C. atatmospheric pressure with a GHSV (gas hourly space velocity) of 900 h⁻¹and a 5 hour time-on-stream (TOS). In the case of the dual catalystsystem, 1 ml of each catalyst separated with glass wool was used.

The supported tungsten oxide catalyst was tested in both the single anddual catalyst systems and the results are shown in Table 4. The highestpropylene selectivity is obtained for a dual catalyst system with10WO₃/Q10 at the top (T) and MFI-2000 at the bottom (B) of the reactor.When 10WO₃/Q10 metathesis catalyst is used in a single-bed catalystsystem, a propylene (C₃═) yield of 31.97 mol. % and a pentene (C₅═)yield of 12.70 mol. % are obtained. These results indicate that thepentenes formed during metathesis of butenes are not completely crackedinto propylene and ethylene. However, the 10WO₃/Q10(T)/MFI-2000 (B)yielded 3.37 mol. % of pentene thus indicating that most of the pentenesformed during the metathesis reaction are cracked into propylene andethylene. Thus, there is a clear advantage of using a dual catalystsystem with the cracking catalyst at the bottom of the catalyst bed.Moreover, when comparing the 10WO₃/Q10(T)/MFI-2000(B) with the reversearrangement of cracking catalyst upstream of metathesis catalyst, the10WO₃/Q10(T)/MFI-2000 (B) yields approximately a 4.5 mol. % increase inpropylene over the MFI-2000(T)/10WO₃/Q10(B) while only yielding slightlyless (˜1.5 mol. %) ethylene (C₂═). Thus, propylene yield is clearlymaximized by using a dual catalyst system with the cracking catalyst atthe bottom of the catalyst bed.

TABLE 4 10WO₃/Q10 MFI-2000 (T) 10WO₃/Q10(T) mixed 10WO₃/Q10 ProductComponent MFI-2000 10WO₃/Q10 MFI-2000 (B) MFI-2000 (B) Conversion 2-C₄═(%) 92.24 70.96 86.35 87.01 86.2 C₂═ 29.39 7.95 23.01 24.76 24.85 C₃═37.56 31.97 45.64 43.77 41.09 1-C₄═ 2.80 10.83 4.78 4.87 4.98Isobutylene 5.72 2.20 9.83 10.01 11.04 C₅═ 2.25 12.70 3.37 3.52 3.59 C₆═0.00 2.17 0.00 0.00 0.00

Calculation Methodologies

The surface area of the samples was measured by nitrogen adsorption at77 K using AUTOSORB-1 (Quanta Chrome). Before adsorption measurements,samples (ca. 0.1 g) were heated at 220° C. for 2 hours under nitrogenflow. The nitrogen adsorption isotherms of catalysts were measured atliquid nitrogen temperature (77 K). The surface areas and pore sizedistributions were calculated by the Brunauer Emmett-Teller (BET) methodand the Barrett-Joyner-Halenda (BJH) method, respectively. The totalpore volume was estimated from the amount of N2 adsorbed at P/PO=0.99.Barret E P, Joyner L J, Halenda P H, J. Am. Chem. Soc. 73 (1951)373-380.

The zeolite samples were characterized by XRD with a Rigaku Mini-flex IIsystem using nickel filtered CuKα radiation (λ=1.5406 Å, 30 kV and 15mA). The XRD patterns were recorded in static scanning mode from 1.2-50°(2θ) at a detector angular speed of 2° min⁻¹ with a step size of 0.02°.

SEM images were measured with a JEOL JSM-5800 scanning microscope at amagnification of 7000. Before taking SEM photographs, the samples wereloaded on a sample holder, held with conductive aluminum tape, andcoated with a film of gold in a vacuum with a Cressington sputterion-coater for 20 seconds with 15 milliAmpere (mA) current.

It should now be understood that various aspects of the systems andmethods of making propylene with the dual catalysts are described andsuch aspects may be utilized in conjunction with various other aspects.

In a first aspect, the disclosure provides a process for production ofpropylene comprising providing a dual catalyst system comprising amesoporous silica catalyst impregnated with metal oxide, and a mordeniteframework inverted (MFI) structured silica catalyst downstream of themesoporous silica catalyst. The mesoporous silica catalyst includes apore size distribution of about 2.5 nm to about 40 nm and a total porevolume of at least about 0.600 cm³/g. The MFI structured silica catalystincludes total acidity of 0.001 mmol/g to 0.1 mmol/g. The process alsocomprises producing propylene from a stream comprising butene viametathesis and cracking by contacting the stream comprising butene withthe dual catalyst system, where the stream comprising butene contactsthe mesoporous silica catalyst before contacting the MFI structuredsilica catalyst.

In a second aspect, the disclosure provides a process of the firstaspect, in which the mesoporous silica catalyst support is produced viawet impregnation or hydrothermal synthesis.

In a third aspect, the disclosure provides a process of either the firstor second aspects, in which the butene stream comprises 2-butene, andoptionally one or more of 1-butene, trans-2-butene, and cis-2-butene.

In a fourth aspect, the disclosure provides a process of any one of thefirst through third aspects, in which the mesoporous silica catalystcatalyzes isomerization of 2-butene to 1-butene followed bycross-metathesis of 2-butene and 1-butene into a metathesis productstream comprising propylene, and the MFI structured silica catalyst is acracking catalyst which produces propylene from C₄ and C₅ olefins in themetathesis product stream.

In a fifth aspect, the disclosure provides a process of any one of thefirst through fourth aspects, in which the metal oxide of the mesoporoussilica catalyst comprises one or more oxides of molybdenum, rhenium,tungsten, or combinations thereof.

In a sixth aspect, the disclosure provides a process of any one of thefirst through fifth aspects, in which the metal oxide of the mesoporoussilica catalyst is tungsten oxide (WO₃).

In a seventh aspect, the disclosure provides a process of any one of thefirst through sixth aspects, in which the mesoporous silica catalyst hasa molar ratio for silica/tungsten oxide of about 5 to about 60.

In an eighth aspect, the disclosure provides a process of any one of thefirst through seventh aspects, in which the mesoporous silica catalystincludes a pore size distribution of from about 2.5 nm to 20 nm.

In a ninth aspect, the disclosure provides a process of any one of thefirst through eighth aspects, in which the mesoporous silica catalysthas a surface area of about 250 m²/g to about 600 m²/g.

In a tenth aspect, the disclosure provides a process of any one of thefirst through ninth aspects, in which the MFI structured silica catalystis free of acidity modifiers selected from the group consisting of rareearth modifiers, phosphorus modifiers, potassium modifiers, andcombinations thereof.

In an eleventh aspect, the disclosure provides a process of any one ofthe first through tenth aspects, in which the mesoporous silica catalysthas a particle size of about 20 nm to about 200 nm.

In a twelfth aspect, the disclosure provides a process of any one of thefirst through eleventh aspects, in which the mesoporous silica catalysthas an individual crystal size ranging from about 10 to about 40 μm.

In a thirteenth aspect, the disclosure provides a process of any one ofthe first through twelfth aspects, in which the MFI structured silicacatalyst is alumina free.

In a fourteenth aspect, the disclosure provides a process of any one ofthe first through thirteenth aspects, in which the MFI structured silicacatalyst is alumina free or alumina containing.

In a fifteenth aspect, the disclosure provides a process of any one ofthe first through fourteenth aspects, in which the MFI structured silicacatalyst has a molar ratio of silica to alumina of about 200 to about3000.

In a sixteenth aspect, the disclosure provides a process of any one ofthe first through fifteenth aspects, in which the MFI structured silicacatalyst has a molar ratio of silica to alumina of about 200 to about3000.

In a seventeenth aspect, the disclosure provides a process of any one ofthe first through sixteenth aspects, in which the MFI structured silicacatalyst has a surface area of at about 300 m²/g to about 425 m²/g.

In an eighteenth aspect, the disclosure provides a process of any one ofthe first through seventeenth aspects, in which the MFI structuredsilica catalyst has a pore size distribution of from about 1.5 nm to 3nm and a pore volume of at about 0.1 cm³/g to about 0.3 cm³/g.

In a nineteenth aspect, the disclosure provides a process of any one ofthe first through eighteenth aspects, in which the MFI structured silicacatalyst has a crystal size of about 10 μm to about 40 μm.

In a twentieth aspect, the disclosure provides a process of any one ofthe first through twentieth aspects, in which the contact between thebutene and the catalyst occurs at a space hour velocity of about 300 toabout 1200 h⁻¹.

In a twenty-first aspect, the disclosure provides a process of any oneof the first through twentieth aspects, in which the contact between thebutene and the catalyst is at a temperature of about 300 to about 600°C.

In a twenty-second aspect, the disclosure provides a process of any oneof the first through twenty-first aspects, in which the contact betweenthe butene and the catalyst is at a pressure of about 1 to about 10bars.

In a twenty-third aspect, the disclosure provides a process of any oneof the first through twenty-second aspects, in which the processachieves at least an 85 mol. % conversion of butene and a propyleneyield in mol. % of the at least 45%.

In a twenty-fourth aspect, the disclosure provides a process of any oneof the first through twenty-third aspects, in which the process achievesat least an 85 mol. % conversion of butene and a propylene yield in mol.% of at least 45%.

In a twenty-fifth aspect, the disclosure provides a process of any oneof the first through twenty-fourth aspects, in which the processachieves a yield of at least a 15 mol. % ethylene.

In a twenty-sixth aspect, the disclosure provides a process of any oneof the first through twenty-fifth aspects, in which the process achievesa yield of at least 20 mol. % ethylene and a propylene yield in mol. %of the at least 45%.

In a twenty-seventh aspect, the disclosure provides a dual catalystsystem for producing propylene from butene, which may be utilized in theprocess of process of any one of the first through twenty-sixth aspects,where the dual catalyst system comprising a metathesis catalyst zone anda cracking catalyst zone downstream of the metathesis catalyst zone. Themetathesis catalyst zone comprises mesoporous silica catalystimpregnated with metal oxide, where the mesoporous silica catalystincludes a pore size distribution of at least about 2.5 nm to about 40nm and a total pore volume of at least about 0.600 cm³/g. The crackingcatalyst zone comprises a mordenite framework inverted (MFI) structuredsilica catalyst, where the MFI structured silica catalyst includes apore size distribution of at least 1.5 nm to 3 nm, and a total acidityof 0.001 mmol/g to 0.1 mmol/g.

In a twenty-eighth aspect, the disclosure provides a dual catalystsystem of the twenty-seventh aspect, in which the metathesis catalystzone and the cracking catalyst zone are disposed in one reactor.

In a twenty-ninth aspect, the disclosure provides a dual catalyst systemof any one of the twenty-seventh or twenty-eighth aspects, in which themetathesis catalyst zone is disposed in a first reactor and the crackingcatalyst zone is disposed in a second reactor downstream of the firstreactor.

In a thirtieth aspect, the disclosure provides a dual catalyst system ofthe thirtieth aspect, in which there is a conduit between the firstreactor and the second reactor.

In a thirty-first aspect, the disclosure provides a dual catalyst systemof any one of the twenty-seventh through thirtieth aspects, in which themesoporous silica catalyst has a molar ratio for silica/metal oxide ofabout 10 to about 50.

In a thirty-second aspect, the disclosure provides a dual catalystsystem of any one of the twenty-seventh through thirty-first aspects, inwhich the metal oxide of the mesoporous silica catalyst is tungstenoxide (WO₃).

In a thirty-third aspect, the disclosure provides a dual catalyst systemof any one of the twenty-seventh through thirty-second aspects, in whichthe MFI structured silica catalyst is alumina free or comprises alumina.

In a thirty-fourth aspect, the disclosure provides a dual catalystsystem of any one of the twenty-seventh through thirty-third aspects, inwhich the MFI structured silica catalyst has a molar ratio of silica toalumina of about 200 to about 3000.

In a thirty-fifth aspect, the disclosure provides a dual catalyst systemof any one of the twenty-seventh through thirty-fourth aspects, in whichthe MFI structured silica catalyst is free of acidity modifiers selectedfrom the group consisting of rare earth modifiers, phosphorus modifiers,potassium modifiers, and combinations thereof.

It should be apparent to those skilled in the art that variousmodifications and variations can be made to the described embodimentswithout departing from the spirit and scope of the claimed subjectmatter. Thus it is intended that the specification cover themodifications and variations of the various described embodimentsprovided such modification and variations come within the scope of theappended claims and their equivalents.

What is claimed is:
 1. A process for production of propylene comprising:contacting a stream comprising butene with a metathesis catalyst in ametathesis catalyst zone, where the metathesis catalyst is a mesoporoussilica catalyst impregnated with metal oxide, passing the streamcomprising butene directly from the metathesis catalyst zone to acracking catalyst zone comprising a cracking catalyst different than themetathesis catalyst, where the cracking catalyst is a mordeniteframework inverted (MFI) structured silica catalyst, contacting thestream comprising butene with the cracking catalyst in the crackingcatalyst zone, where the stream comprising butene contacts themetathesis catalyst before contacting the cracking catalyst; and passinga product stream out of the cracking reaction zone, the product streamcomprising propylene.
 2. The process of claim 1 where the streamcomprising butene includes 2-butene.
 3. The process of claim 1 where thestream comprising butene is contacted with the metathesis catalyst andthe cracking catalyst at a space hourly velocity of from 300 per hour to1200 per hour.
 4. The process of claim 1 where the stream comprisingbutene is contacted with the metathesis catalyst and the crackingcatalyst at a temperature of from 300 degrees Celsius to 600 degreesCelsius and a pressure of from 1 bar to 10 bars.
 5. The process of claim1 where the metathesis catalyst catalyzes isomerization of 2-butene to1-butene followed by cross-metathesis of 2-butene and 1-butene into ametathesis product stream comprising propylene, and the crackingcatalyst produces propylene from C₄ or C₅ olefins in the metathesisproduct stream.
 6. The process of claim 1 where the metathesis catalystincludes a pore size distribution of from 2.5 nanometer (nm) to 40 nmand a total pore volume of at least 0.600 cubic centimeters per gram(cm³/g).
 7. The process of claim 1 where the metal oxide of themesoporous silica catalyst comprises one or more oxides of molybdenum,rhenium, tungsten, or combinations thereof.
 8. The process of claim 1where the metal oxide of the mesoporous silica catalyst is tungstenoxide (WO₃).
 9. The process of claim 8 where the mesoporous silicacatalyst has a molar ratio of silica to tungsten oxide of from 5 to 60.10. The process of claim 1 where the mesoporous silica catalyst has asurface area of from 250 square meters per gram (m²/g) to 600 m²/g. 11.The process of claim 1 where the mesoporous silica catalyst has aparticle size of from 20 nm to 200 nm and an individual crystal size offrom 1 micrometer (μm) to 100 μm.
 12. The process of claim 1 where theMFI structured silica catalyst has a total acidity of from 0.001millimole per gram (mmol/g) to 0.1 mmol/g.
 13. The process of claim 1where the MFI structured silica catalyst has a pore size distribution ofat least 1.5 nm to 3 nm.
 14. The process of claim 1 where the MFIstructured silica catalyst has a pore volume of from 0.1 cm³/g to 0.3cm³/g.
 15. The process of claim 1 where the MFI structured silicacatalyst is alumina free.
 16. The process of claim 1 where themetathesis catalyst zone and the cracking catalyst zone are disposedwithin a first reactor and a second reactor, respectively, and a directconduit extends between the first reactor and the second reactor. 17.The process of claim 1 where the metathesis catalyst zone and thecracking catalyst zone are disposed within one reactor.